US6617276B1 - Hydrocarbon trap/catalyst for reducing cold-start emissions from internal combustion engines - Google Patents
Hydrocarbon trap/catalyst for reducing cold-start emissions from internal combustion engines Download PDFInfo
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- US6617276B1 US6617276B1 US09/621,596 US62159600A US6617276B1 US 6617276 B1 US6617276 B1 US 6617276B1 US 62159600 A US62159600 A US 62159600A US 6617276 B1 US6617276 B1 US 6617276B1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
- B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
- B01D53/9445—Simultaneously removing carbon monoxide, hydrocarbons or nitrogen oxides making use of three-way catalysts [TWC] or four-way-catalysts [FWC]
- B01D53/945—Simultaneously removing carbon monoxide, hydrocarbons or nitrogen oxides making use of three-way catalysts [TWC] or four-way-catalysts [FWC] characterised by a specific catalyst
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the alkali- or alkaline earth metals or beryllium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
- B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
- B01D53/944—Simultaneously removing carbon monoxide, hydrocarbons or carbon making use of oxidation catalysts
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1021—Platinum
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1023—Palladium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1025—Rhodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/204—Alkaline earth metals
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/50—Zeolites
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/90—Physical characteristics of catalysts
- B01D2255/912—HC-storage component incorporated in the catalyst
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/12—Improving ICE efficiencies
Definitions
- This invention relates to hydrocarbon trap/catalysts that are effective for trapping hydrocarbons and oxidizing the trapped hydrocarbons in an exhaust gas.
- the present invention is directed to enhancing oxidation of adsorbed hydrocarbons when the hydrocarbon trap/catalyst reaches a temperature at which the trapped (adsorbed) hydrocarbons are released.
- U.S. Pat. No. 3,699,683 discloses an adsorbent bed placed after both a reducing catalyst and an oxidizing catalyst. That patent also discloses that when the exhaust gas stream is below 200° C., the gas stream is directed through the reducing catalyst then through the oxidizing catalyst and finally through the adsorbent bed, thereby adsorbing hydrocarbons on the adsorbent bed.
- the gas stream which is discharged from the oxidation catalyst is divided into a major and minor portion.
- the major portion is discharged directly into the atmosphere.
- the minor portion is passed through the adsorbent bed, whereby unburned hydrocarbons are desorbed, and the resulting minor portion containing the desorbed unburned hydrocarbons is then passed into the engine where the desorbed unburned hydrocarbons are burned.
- U.S. Pat. No. 5,078,979 Another patent disclosing the use of both an adsorbent material and a catalyst composition to treat an automobile engine exhaust stream, especially during the cold-start period of engine operation, is U.S. Pat. No. 5,078,979.
- the adsorbent is a particular type of molecular sieve and the catalyst material which may be dispersed in the adsorbent may be a platinum group metal.
- WO 97/22404 discloses the use of an ion exchange reaction to alter the adsorption characteristics of a zeolite, thereby forming a basic zeolite said to be useful for adsorbing hydrocarbons from-exhaust streams.
- the ion exchange reaction takes place by mixing an alkaline metal or alkaline earth metal salt (sodium, calcium and magnesium are specifically disclosed) in an aqueous solution with the zeolite for a sufficient time and temperature to cause ion exchange. Typical reaction times range from 0.5 to 4.0 hours at from ambient up to 100° C. and more typically 50 to 75° C.
- the exchanged zeolite is then filtered and washed with water and dried.
- the basic zeolite can be formed into a slurry and then coated on to a carrier substrate.
- the present invention pertains to a hydrocarbon trap/catalyst, i.e. a hydrocarbon adsorbing material in which hydrocarbons are adsorbed at a low exhaust gas temperature characteristic of an engine start-up condition.
- this material is impregnated with an active metal to enhance oxidation of the hydrocarbons as the hydrocarbons are desorbed from the material at an elevated temperature characteristic of normal engine exhaust conditions.
- the invention optionally further comprises one or more layers of a support material impregnated with one or more platinum group metal catalysts, in combination with the impregnated hydrocarbon trap catalyst of the present invention.
- the present invention differs from prior hydrocarbon trap/catalysts materials by providing an active metal deposited on and in intimate contact with the hydrocarbon adsorbent material but with little or no chemical reaction between the active metal and the adsorbent. While enhancing oxidation of hydrocarbons, this active metal does not affect the adsorption characteristics of the material.
- the composition of the present invention typically comprises (a), as the hydrocarbon adsorbent material, a zeolite which is effective for adsorbing hydrocarbons from an engine exhaust and (b) an active metal in intimate contact with the zeolite.
- the invention optionally further comprises one or more layers of (c) a three way or oxidation catalyst that includes at least one platinum group metal (PGM) and preferably includes a combination of platinum group metals. Most preferably that combination comprises platinum, palladium and rhodium in a weight ratio collectively of about 12:5:1.
- the active metal useful for the above purposes is essentially any alkaline metal or alkaline earth metal, such as potassium, rubidium, cesium, beryllium, magnesium, calcium, barium and strontium. Cesium is preferred.
- the active metal is deposited in intimate contact with the hydrocarbon adsorbent (zeolite, for example) by pouring, dipping or spraying a soluble salt solution of the active metal onto the adsorbent, which is then heated to dryness.
- hydrocarbon adsorbent zeolite, for example
- the hydrocarbon adsorbent may be first deposited (prior to impregnation with the active metal) on a catalyst substrate, such as an inert monolithic or foam structure or inert pellets or beads.
- zeolite is the preferred hydrocarbon adsorbent in the present invention
- other hydrocarbon adsorbents may also be useful.
- amorphous silica and certain forms of carbon or activated carbon, particularly including refractory forms of carbon such as C n fullerenes.
- the present invention comprises an improved hydrocarbon trap composition including a hydrocarbon-adsorbing material, such as zeolite, which is impregnated with an active metal, such that oxidation of desorbed hydrocarbons is enhanced.
- a hydrocarbon-adsorbing material such as zeolite
- an active metal such that oxidation of desorbed hydrocarbons is enhanced.
- Such impregnation may be effected by contacting a dry zeolite with a soluble salt solution, such as an acetate or a nitrate of an active metal, namely an alkaline metal or alkaline earth metal, particularly cesium, and drying the wet zeolite with heating to remove water, leaving the metal in intimate contact with the zeolite but avoiding ion exchange therewith.
- a similar effect may be produced by slurrying zeolite alone in water and depositing the slurry on a monolithic catalyst substrate, drying the slurry to leave the zeolite in intimate contact with the substrate and then dipping, pouring or spraying an active metal solution over the zeolite substrate and drying that solution, with heat, as above, to leave active metal in intimate contact with the zeolite on the substrate.
- Natural zeolites include faujasites, clinoptilolites, mordenites, and chabazites.
- Synthetic zeolites include ZSM-5, beta, Y, ultrastable-Y, mordenite, ferrierite, and MCM-22, with ZSM-5 and beta preferred.
- the SiO 2 :Al 2 O 3 ratio for these materials is typically in the range of 2-1000, with a preferred SiO 2 :Al 2 O 3 ratio of 30-300.
- the active metal acts as a catalyst for breaking C—H bonds in the hydrocarbons.
- suitable active metals which are believed to be useful for this purpose, are alkaline metals and alkaline earth metals, such as lithium, sodium, potassium, rubidium, cesium, beryllium, magnesium, calcium, barium and strontium. Of these, cesium is preferred.
- the active metal-impregnated zeolite is a coating on a ceramic or metallic monolithic catalyst support or substrate which serves as an inert carrier for the active metal-containing zeolite and any subsequent catalyst coatings.
- Such support substrates may be porous or non-porous.
- the binder material is typically alumina or colloidal silicon dioxide.
- the binder is typically added in an amount of about 10-25% of the total weight of the zeolite to form a semi-solid mixture.
- the mixture is milled to obtain a nominal particle size of 1.0-20.0 microns, typically 4.5-5.0 microns. Once the desired particle size is achieved, the mixture is heated in flowing air at a temperature of in the range of 400° C.-600° C., typically about 500° C., for 30-90 minutes, typically 30-60 minutes, until it is essentially dry.
- the zeolite slurry may be applied to a support substrate, such as a monolith catalyst base of the type used in automotive exhaust systems, by pouring or spraying the zeolite slurry onto the support substrate or by dipping the support substrate into the zeolite slurry to form a first layer coating. If applied to a support substrate, the zeolite and support substrate are heated, as described above, until the zeolite firmly adheres to the inert carrier and any excess water has been evaporated.
- the amount of zeolite and binding material deposited should be at least 0.2, and preferably more than 1.0, but possibly as much as 4.0 g/in 3 (g per 16.4 cm 3 ).
- Impregnating at least one active metal onto the surface of the zeolite is accomplished at room temperature followed by drying at an elevated temperature.
- a solution of the active metal e.g. an aqueous solution of CsNO 3 , CsC 2 H 3 O 2 or some other soluble form of the active metal; 0.64 M CsNO 3 in the example below
- the zeolite or substrate on which zeolite has been deposited may be dipped into the solution.
- the zeolite is saturated with the active metal solution, by repeated contact steps if necessary, until enough of the solution has been absorbed in the zeolite to deposit a calculated amount of the active metal, taking into account the amount of solution absorbed and the concentration of the salt in the original solution.
- the amount of metal deposited should be at least 0.19, and preferably more than 3.7, but possibly as much as 16.2 weight % of active metal on the zeolite.
- the actual contact time to achieve this impregnation may be relatively short, on the order of 0.1 to 5 minutes, but generally is in the range of 0.5 to 2 minutes. One half minute of contact time is typically sufficient.
- the active metal solution/zeolite mixture is heated in flowing air at a temperature of about 400° C.-600° C., with 500° C. particularly preferred, for 30-90 minutes, with 30-60 minutes preferred.
- the zeolite and active metal solution mixture is heated to dryness, whereupon some or all of the metal in the active metal salt (typically a nitrate or acetate) is decomposed into either its metallic state or to a metal compound which is in intimate contact with the zeolite. Because the original impregnation occurred at room temperature and the subsequent heating occurred with relatively little water present, relatively little chemical interaction occurs between the active metal and the zeolite adsorbent in this impregnation process.
- the active metal-impregnated zeolite is formed on a monolithic catalyst substrate and forms a first coating of a multi-layer catalyst structure.
- the overall composition of one such catalyst structure is described below.
- the second and succeeding catalyst layers may be produced in accordance with the invention disclosed in U.S. Pat. No. 6,022,825—Andersen et al. (the '825 patent), of common assignment herewith, the entirety of which is incorporated herein by reference.
- the zirconium stabilized ceria of the second.layer may be replaced with zirconium stabilized manganate, containing 20-70% zirconium oxide, and typically containing 40-65% zirconium oxide.
- An optional third catalyst layer useful in the present invention comprises a washcoat which is also derived from one or more component slurries.
- This third catalyst layer which when in combination with the active metal-impregnated zeolite of the present invention, enhances oxidation of hydrocarbons may be produced in accordance with the invention disclosed in PCT application WO 99/67020, also of common assignment herewith and also incorporated herein by reference.
- the optional third layer, together with the optional second layer comprises, as the PGM constituents, platinum, palladium and rhodium in a weight ratio on the order of 12:5:1.
- the catalyst structure generally comprising the comparative composition set forth below in Hydrocarbon Trap/Catalyst 1 was tested against an exemplary catalyst structure/composition of the present invention, set forth below as Hydrocarbon Trap/Catalyst 2.
- Hydrocarbon Trap/Catalyst 2 contains cesium in the first layer 1; Comparative Hydrocarbon Trap/Catalyst 1 does not.
- Hydrocarbon Trap/Catalyst 1 comprises a zeolite hydrocarbon adsorbent as Layer 1, on a monolith, subsequently coated with catalyst Layers 2 and 3.
- Layer 1 was prepared by blending ZSM-5 and de-ionized water to form a slurry in a proportion of 1:2. Silicon dioxide was added to the slurry in an amount approximately equal to 10% by weight of the ZSM-5.
- the zeolite slurry was then coated on a conventional cordierite honeycomb monolith having 400 holes per square inch (per 6.45 square cm) by dipping the monolith into the slurry. The excess zeolite was blown off with compressed air, and the zeolite and monolith were subsequently heated in flowing air for 40 minutes at 500° C. to drive off excess water and adhere the zeolite to the surface of the monolith.
- the total loading was 1.65 g per in 3 (per 16.4 cm 3 ) with a composition by weight of 90.91% ZSM-5 and 9.09% silicon dioxide.
- Layer 2 was prepared in accordance with the '825 patent.
- the total loading was 3.399 g/in 3 (per 16.4 cm 3 ) with a composition by weight of 67.67% La-stabilized alumina, 23.54% Zr-stabilized ceria, 2.71% NiO, 2.38% neodymium oxide, 2.62% Pt, and 1.09% Pd.
- Layer 3 was prepared in accordance with WO 99/67020. The total loading was 1.358 g/in 3 (per 16.4 cm 3 ) with a composition by weight of 73.64% Ce-stabilized zirconia, 25.77% La-stabilized alumina, and 0.59% Rh.
- Hydrocarbon Trap/Catalyst 2 is a layered catalyst structure similar to that of Hydrocarbon Trap Catalyst 1, but differing in that cesium is impregnated on the zeolite surface of Layer 1.
- Cesium was impregnated on the surface of the zeolite by pouring a 0.64 M solution of cesium nitrate (CsNO 3 ) onto the zeolite coated monolith at room temperature. The wet zeolite was then dried in heated flowing air for 40 minutes at 500° C. The total loading was 1.82 g per in 3 (per 16.4 cm 3 ) with a composition by weight of 82.42% ZSM-5, 9.35% cesium nitrate, and 8.24% silicon dioxide. Layers 2 and 3 were subsequently coated over layer 1 as described above.
- the catalyst structures were then heated from 60° C. to 500° C. at 50° C. per minute in a flowing gas stream of the same compositions as that used to simulate cold-start exhaust gas, but modified by the omission of hydrocarbons.
- the gas exiting the catalyst structures was continuously sampled and analyzed using both a flame ionization-detection system and infra-red detectors. The results of the tests are indicated in Table 1 below.
- % Hydrocarbon Oxidized is based on the quantity of hydrocarbon adsorbed on the catalyst in the first minute of the test versus the quantity of the hydrocarbon oxidized in the 9 minute period during which the catalyst is exposed to the warmer simulated exhaust gas mixture; the latter is calculated from the quantity of unoxidized carbon exiting the catalyst in the second part of the test, as compared to that adsorbed in the catalyst in the first part of the test.
- Results shown in Table 1 demonstrate that the amount of hydrocarbons removed from the gas stream by the cesium-impregnated zeolite is on the order of twice that of the catalyst structure without the cesium, both with CO present and without.
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- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Exhaust Gas After Treatment (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Description
TABLE 1 |
The % yield is calculated as |
(% hydrocarbon adsorbed *% hydrocarbons oxidized)/100. |
Hydrocarbon | % | % | ||
Trap/ | Test | Hydrocarbons | Hydrocarbons | % |
Catalyst | Condition | Adsorbed | Oxidized | Yield |
1 | Run 1 (w/ CO) | 50.3 | 17.0 | 8.6 |
2 | Run 1 (w/ CO) | 46.5 | 29.8 | 13.9 |
1 | Run 2 (w/o CO) | 46.0 | 17.8 | 8.2 |
2 | Run 2 (w/o CO) | 51.8 | 36.9 | 19.1 |
Claims (23)
Priority Applications (16)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/621,596 US6617276B1 (en) | 2000-07-21 | 2000-07-21 | Hydrocarbon trap/catalyst for reducing cold-start emissions from internal combustion engines |
NZ523737A NZ523737A (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition |
PCT/GB2001/003188 WO2002007859A2 (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition |
MXPA03000595A MXPA03000595A (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition. |
EP01949716A EP1301264B1 (en) | 2000-07-21 | 2001-07-20 | Automotive exhaust system comprising a hydrocarbon trap/catalyst |
KR1020037000933A KR100795444B1 (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon Trap / Catalyst Composition |
JP2002513587A JP4873822B2 (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap / catalyst composition |
CA002416425A CA2416425A1 (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition |
BRPI0112615-6B1A BR0112615B1 (en) | 2000-07-21 | 2001-07-20 | catalyst structure, and method of producing and using such a catalyst structure. |
DE60108505T DE60108505T2 (en) | 2000-07-21 | 2001-07-20 | VEHICLE EXHAUST SYSTEM WITH HYDROCARBON CATH / CATALYST |
ES01949716T ES2234853T3 (en) | 2000-07-21 | 2001-07-20 | CAR EXHAUST SYSTEM, WITH CATALYST / HYDROCARBON TRAP. |
PL01365045A PL365045A1 (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition |
AU2001270835A AU2001270835B2 (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition |
AU7083501A AU7083501A (en) | 2000-07-21 | 2001-07-20 | Hydrocarbon trap/catalyst composition |
AT01949716T ATE287283T1 (en) | 2000-07-21 | 2001-07-20 | VEHICLE EXHAUST SYSTEM WITH HYDROCARBON Scavenger/CATALYST |
NO20030277A NO20030277L (en) | 2000-07-21 | 2003-01-20 | Hydrocarbon separator / catalyst composition |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/621,596 US6617276B1 (en) | 2000-07-21 | 2000-07-21 | Hydrocarbon trap/catalyst for reducing cold-start emissions from internal combustion engines |
Publications (1)
Publication Number | Publication Date |
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US6617276B1 true US6617276B1 (en) | 2003-09-09 |
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ID=24490826
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US09/621,596 Expired - Lifetime US6617276B1 (en) | 2000-07-21 | 2000-07-21 | Hydrocarbon trap/catalyst for reducing cold-start emissions from internal combustion engines |
Country Status (15)
Country | Link |
---|---|
US (1) | US6617276B1 (en) |
EP (1) | EP1301264B1 (en) |
JP (1) | JP4873822B2 (en) |
KR (1) | KR100795444B1 (en) |
AT (1) | ATE287283T1 (en) |
AU (2) | AU2001270835B2 (en) |
BR (1) | BR0112615B1 (en) |
CA (1) | CA2416425A1 (en) |
DE (1) | DE60108505T2 (en) |
ES (1) | ES2234853T3 (en) |
MX (1) | MXPA03000595A (en) |
NO (1) | NO20030277L (en) |
NZ (1) | NZ523737A (en) |
PL (1) | PL365045A1 (en) |
WO (1) | WO2002007859A2 (en) |
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US20030129098A1 (en) * | 2001-12-04 | 2003-07-10 | Tetsuo Endo | Internal combustion engine exhaust gas purification device |
US20030147796A1 (en) * | 2001-12-27 | 2003-08-07 | Nissan Motor Co., Ltd. | Exhaust gas purifying catalyst and method for purifying exhaust gas |
US20040038801A1 (en) * | 2001-10-16 | 2004-02-26 | Hiroto Kikuchi | Catalyst using metal carrier and manufacturing method thereof |
US20040180782A1 (en) * | 2003-03-10 | 2004-09-16 | Cataler Corporation | Exhaust-gas purifying catalyst |
US20070045101A1 (en) * | 2005-07-06 | 2007-03-01 | Rochester Institute Of Technology | Self-regenerating particulate trap systems for emissions and methods thereof |
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US20110124489A1 (en) * | 2006-09-19 | 2011-05-26 | Denso Corporation | Carbon-based material combustion catalyst, manufacturing method of the same, catalyst carrier, and manufacturing method of the same |
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GB2484911A (en) * | 2010-10-22 | 2012-05-02 | Johnson Matthey Plc | NOx storage component comprising caesium silicate and a platinum group metal |
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US8926910B2 (en) | 2012-02-07 | 2015-01-06 | Ford Global Technologies, Llc | Hydrocarbon trap for reducing cold-start engine emissions |
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DE102016102028A1 (en) | 2015-02-06 | 2016-08-11 | Johnson Matthey Public Limited Company | Three-way catalytic converter |
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US10125650B1 (en) * | 2017-10-26 | 2018-11-13 | Hyundai Motor Company | Exhaust gas purification apparatus |
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Also Published As
Publication number | Publication date |
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NZ523737A (en) | 2004-07-30 |
MXPA03000595A (en) | 2003-10-06 |
ATE287283T1 (en) | 2005-02-15 |
MX232811B (en) | 2005-12-09 |
NO20030277L (en) | 2003-03-20 |
EP1301264A2 (en) | 2003-04-16 |
DE60108505D1 (en) | 2005-02-24 |
JP2004504130A (en) | 2004-02-12 |
BR0112615B1 (en) | 2013-06-11 |
CA2416425A1 (en) | 2002-01-31 |
AU2001270835B2 (en) | 2006-06-01 |
KR20030017646A (en) | 2003-03-03 |
AU7083501A (en) | 2002-02-05 |
NO20030277D0 (en) | 2003-01-20 |
PL365045A1 (en) | 2004-12-27 |
DE60108505T2 (en) | 2005-06-23 |
WO2002007859A2 (en) | 2002-01-31 |
EP1301264B1 (en) | 2005-01-19 |
JP4873822B2 (en) | 2012-02-08 |
WO2002007859A3 (en) | 2002-08-08 |
BR0112615A (en) | 2003-06-10 |
KR100795444B1 (en) | 2008-01-16 |
ES2234853T3 (en) | 2005-07-01 |
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